Production of synthetic lubricants from alpha-olefins through a ternary catalytic system

ABSTRACT

Synthetic, high quality lubricating oils are produced through the polymerization of a single alpha-olefin or a mixture of alpha-olefins from &#39;&#39;&#39;&#39;wax-cracking&#39;&#39;&#39;&#39; having the formula R - CH CH2 wherein R is an alkyl radical containing from 2 to 16 C atoms, by the use, in a dry nitrogen atmosphere, of a catalyst system constituted by a compound of a transition metal selected from groups IV to VIII of the periodic system (e.g., TiCl4) and by two coordinate anionic cocatalysts, one of which is an aluminum compound of inorganic nature devoid of any metal-carbon bond and consisting of a polyiminic linear polymer (e.g., a polyimine alane represented by the formula:   WHEREIN R is alkyl, aryl or cycloalkyl and n is a whole number from 4 to 25) and the other of which is an aluminum compound of the conventional Ziegler type with a metal-carbon link (e.g., an aluminum alkyl sesquichloride or an aluminum dialkyl monochloride.

United States Patent Girotti et al.

[ May 20, 1975 41 PRODUCTION OF SYNTHETIC LUBRICANTS FROM ALPHA-OLEFINS THROUGH A TERNARY CATALYTIC SYSTEM [75] lnventors: Pierleone Girotti; Renato Tesei;

Telemaco Floris, all of San Donato Milanese, ltaly [73] Assignee: Snamprogetti S.p.A., San Donato Milanese, Italy [22] Filed: Feb. 15, 1973 [21] Appl. No.: 332,627

[30] Foreign Application Priority Data Feb. 15, 1972 Italy 20564/72 [52] US. Cl 260/683.l5 D; 252/59; 252/431 N;

- 260/6839 [51] Int. Cl. C07c 3/10 [58] Field of Search 260/683.15 D; 252/59, 431 N [56] References Cited UNITED STATES PATENTS 3,156,736 11/1964 Southern et al. 260/683.15 D 3,259,668 7/1966 Antonsen 260/683.15 D 3,467,639 9/1969 Marconi et a1. 252/429 A 3,489,736 1/1970 Takahashi et al 252/431 N 3,798,284 3/1974 Tesei et al. 260/683.15 D

Primary Examiner-Paul M. Coughlan, Jr. Attorney, Agent, or FirmRalph M. Watson TiC1 and by two coordinate anionic cocatalysts, one

of which is an aluminum compound of inorganic nature devoid of any metal-carbon bond and consisting of a polyiminic linear polymer (e.g., a polyimine alane represented by the formula:

AI-N

wherein R is alkyl, aryl or cycloalkyl and n is a whole number from 4 to 25) and the other of which is an aluminum compound of the conventional Ziegler type with a metal-carbon link (e.g., an aluminum alkyl sesquichloride or an aluminum dialkyl monochloride.

8 Claims, No Drawings PRODUCTION OF SYNTHETIC LUBRICANTS FROM ALPHA-OLEFINS THROUGH A TERNARY CATALYTIC SYSTEM The present invention relates to the production of synthetic lubricating oils through polymerization of single pure alpha-olefins or of commercial mixtures of alpha-olefins coming from wax crackingwith a catalytic system consisting of a catalyst and of two cocatalysts.

The catalytic systems to which we refer in the present invention comprise three components one of said components being a halide of a transition metal. Generally in such catalytic systems the compounds of the transition metals are named catalysts and the remaining components are named cocatalysts even if it is understood that the effect of these systems depends on the interaction of all the components and that no distinction can be made about the function of each component, and it is settled that the term cocatalyst is used for the purpose of a better understanding in the specification and in the claims of'the text itself.

It is well known that in mineral lubricating oils, to increase the viscosity index the so named improvers of the viscosity index are employed, which are polymers having a very high molecular weight; however during the running of the motor they depolymerize and consequently the oils containing them are made worse with respect to both the viscosity and the viscosity index.

That disadvantage has been overcome by using synthetic lubricating oils, which possess themselves the characteristic of a high viscosity index, which does not decrease during use even after a long period of running. The production of such synthetic oils has been carried out mainly by polymerizing the alpha-olefins. In the bebeen resorted to, such as the one described in the US.

Pat. No. 3,113,167 according to which the lubricating oil is produced in two stages, in the first of which there is employed a ratio of the catalyst components which makes possible obtaining solid polymers and in a second stage, byvarying the above mentioned ratio, liquid polymers are obtained, which dissolve the first ones, and in this way it is possible to obtain oils of the desired viscosity. It is obvious however that this manner of proceding is very complex. v

A further not negligible disadvantage of, the mentioned catalysts is represented by the time required by the polymerization which ranges from 8 to 20 hours, usually 16-23 hours.

Now is has been found that synthetic oils of a high viscosity index and suitable viscosity may be prepared, without the mentioned disadvantages through the process of this invention, consisting in a polymerization either of pure normal-alpha-olefins or of commercial mixtures of alpha-olefins coming from the wax cracking and having the general formula R-CI-I CH where R is an alkyl radical containing 2-16 carbon atoms. Said polymerization is effected by means of a catalytic system, consisting of a catalyst comprising a compound of a transition metal from the IV to the VIII group of the periodic system and of two coordinated anionic co-catalysts, one of the two cocatalysts being an aluminum compound'of inorganic nature, namely utterly devoid of a metal-carbon link, the other one being an aluminium compound of the conventional Ziegler type with metal-carbon link. The co-catalystof inorganic nature consists of a polyiminic linear polymer (polyimine alane or PIA) having the formula:

-where n is a whole number not higher than 50,"preferapermits obtaining polymers which are comprised, as to viscosity, in the field of the lubricating oils without using hydrogen in the role of controller and regulator of the polymerization according to the method of the above Italian Patent application where however different feeds were used, namely by operating in a nitrogen atmosphere; this occurs with -all the types of olefins, both in the case in which they are pure alpha-olefins (for instance l-decene) and when they are commercial alpha-olefins (for instance C C coming from wax cracking. I

Through the process of this invention the use of hy drogen is not required and moreover the monomer ldecene which does not take part in the reaction does not undergo any hydrogenation and it is susceptible of further polymerization.

The two co-catalysts, namely the PIA (polimine alane) and the compound containing the metal-carbon bond, which reduce the compound of the transition metal, are in a molar ratio which ranges from 60/40 to 90/10 according to the boiling range and to the purity of the alpha-olefins of the feed. Preferably the ratios /30 and /20 are used. Also the ratio, through which the catalytic complex between PIA and the transition metal compound is formed, must be well defined; it may vary from 1.1 to 1.7 being employed preferably in ratios from 1.2 to 1.3. By varying suitably the two above-mentioned molar ratios, it is possible to obtain The feed alpha-olefins must be subjected to deaeration and to dehydration and/or to a pretreating of purification which may be carried out in different ways: with the some exhaust catalyst, with anhydrous TiCl lubricating oils over a wide range of viscosity, from 10 with anhydrous A1Cl with FeSO and H 80 through cSt to 30 est, and also more at l0 percolation on silica and/or molecular sieves and so on.

A8 to the molar ratio between the mp Then the olefins are maintained, after deaeration and mining the metal-carbon bend and the compound of final dehydration in an atmosphere of dry nitrogen. the transition metal, the value 1 has been fixed. AS The compositions of the alpha olefins used as feed in compound of the transition metal TiCl is preferably h present i ti are th f ll in employed, it being possible to employ TiCl or the compounds of vanadium as VC1 VOC1 a.s.o. As noted above the process of the present lnventlon A) ggz fi the linear alphwolefins 97% by WL ls particularly appllcable to the slngle pure alpha- Specific gm), at 0.741 olefins or to their mixtures, obtained from the Wax l5 Refraction index n,,"" 1.4232 cracking of the paraffin, for instance in the range from B) |pha o|efins C4 [0 C5, from C6 to C8, from C7 (0 C9, from C3 t0 C C9-C1, from wax cracking up to C 0... namely the normal industrial production gg'g g j gf ggg gfgg fs; W 2 l fi Distribution of C carbon atom 45% The polymerization reaction is effected preferably by 20 p q q y 0-742 W Refraction lndex, n 1.4240

permitting the catalyst to form in sltu namely in the Molecular weight 32 same olefins; in these conditions it is possible to oper- Bromine number. g g ate in the absence or in the presence of a solvent and in the last case oils are obtained which present, with re- Al th s l t whi h are employed must be despect to the ones obtained in the absence of solvents, d, d h d d d i i d i ah atmosphere lower viscosities. of dry nitrogen. Similarly to the feed olefins and to the By operating on the contrary with the catalyst presolvents, all the components of the catalytic system are formed in the solvent, yields of oils which are remarki i d i a d nitrogen atmosphere T n y lower are Obtaihedduced through the process of this invention is not satu- The hydrocarbons which y he used as Solvents are rated, containing about a double bond per molecule; the conventional organic solvents: the aromatics such it is then subjected to a hydrogenation with a come. as benzene, toluene, xylene, and their derivatives; haloi catalyst containing Pd or P M or C M i genated hydrocarbons, Such as ohlorobenlehe fluoroorder to remove the residual unsaturation. Hereinafter benzene and So i the Saturated hydrocarbons Such as as examples and not as limitations some illustrations of pentanes, hexanes, heptanes, octanes, decanes and the h present i ti are reported,

0 clo araffins such as cyclo hexane, methyl cyclohexaiie aiid so on. EXAMPLE I AlSO mixtures 0f the said hydrocarbons may be used. In a 1 reactor, provided with a stirrer and a jacket Generally, the Selection of the Solvent is made y heal for liquid circulation, accurately dried and deaerated ihg in mind that it must have a boiling Pohlt Such that and flushed with dry nitrogen, there were introduced in the feed olefins and the obtained polymers are easily h f ll i order 350 (259 f 97% Ld separable by distillation. 6.80 cc of a 2.23 molar solution of TiC1 5.30 cc of a The amount of solvent may reach a volume which 0,84 molar solution of Et Cl and 13.80 cc of a 1 may be up to 10 times that of the olefins. molar solution of poly (N-isopropyl imine alane).

The temperature of Polymerization in the Process in The ratio by weight olefine/TiCl was 90. The reducquestion ranges from 0 to 200C, prefer ly between tion of TiCl was ascribed as 70% to the polyimine 15 and 80C. The effect of the temperature is different alane i h a molar ratio Al/Ti 1,3) d 30% to h l according to the use of a pure single alpha-olefin or of aluminum sesquichloride (with a molar ratioAl/Ti mixtures of alpha-olefins Coming from th 1.0). Then we stirred at 25C temperature for 5 hours. cracking. With the first ones by increasing the tempera- At the end the catalyst was deactivated by adding isoture a minor yield of oil is obtained, and the viscosity propyl alcohol and then the oily phase was washed with is higher. The second ones present differences which, diluted l-lCl and subsequently with water till neutralizaby varying the temperature, are less remarkable. tion was complete.

The ratio by weight olefin/compound of the transi- After separating the water phase the oily phase was tion metal, employed in the process of this invention distilled at atmospheric pressure to remove the olefin, may be in the range between 5 and 500, preferably bewhich did not react and subsequently the distillation tween 50 and 150. Such a ratio varies according to the was carried out at reduced pressure. boiling range and to the purity of the feed alpha-olefins. By cutting at a top temperature, under atmospheric The reaction time may reach up to 5 hours. By using pressure, of 400C, 44 g of dimer and 176 g of oil were the catalytic system of the invention the reaction vesobtained, the oil having the boiling point higher than sels after being thoroughly cleaned and dried must be 400C (400C+). flushed with an inert dried gas, for instance, with nitro- The total conversion with reference to the fed olefins gen, was of 84.9% b.w. and the yield in oil was of 68% b.w.

TABLE 1 Characteristics Method 400x: oil

Specific gravity at 20C ASTM 1481 0.8337 Refraction Index, n ASTM D 1747 I 1.4678 Kinematic viscosity at 210F. cSt ASTM D 445 19.14

TABLE 1 Continued Characteristics Method 400C oil Kinematic viscosity at 100F, cSt ASTM D 445 121.7 Viscosity lndex ASTM D 2270 l40/A 188/B Pouring point, C ASTM D 97 50 Ramsbottom carbon'rcsidue, 7r b.w. ASTM D 524 0.03 Neutralization point, mg KOH/g ASTM D 974 0.04

lodine number g/lOO g LP. 48 40 Molecular weight vapor pressure osmometer 650 The above results show that by varying the ratio Al/Ti relative to the alane from 1.3 (of the Example 1 to 1.0 we obtained oils with lower viscosity.

EXAMPLE 3 In a 1 liter reactor provided with a stirrer, dried, deaerated and flushed with dry nitrogen we introduced in the following order 350 cc (259 g) of 97% l-decene, 6.80 cc of a 2.23 molar solution of TiC1.,, 5.40 cc of 0.84 molar solution of AlEt Cl and 15.90 cc ofa 1.0

TABLE II Characteristics Method A 400C hydrogenated oil Specific gravity ASTM D 1481 0.8323 Refraction lndex, n ASTM D 1747 1.4664

Kinematic viscosity at 210F, cSt Kinematic viscosity at 100F. cSt Viscosity lndex ASTM D 445 19.94 ASTM D 445 130.0 ASTM D 2270 1391A 186/B Pour point, "C ASTM D 97 50 Ramsbottom carbon residue 70 b.w. ASTM D 524 0.03 Neutralization mg KOl-l/g ASTM D 974 0.04 Iodine number, g/100 g LP. 48 0.3 Molecular weight V. pressure 670 osmometre EXAMPLE 2 35 molar solution of po1y(N-isopropyliminoalane).

The ratio b.w. olefines/TiCL, was 90. The reduction Into a 1 liter reactor, provided with a stirrer, dried,

of the T1Cl was attributed for the 70% to the deaerated, flushed with dry nitrogen we introduced in the following Order, 350 CC (259 g) of 97% Ldecene, polyimmoalane (having a molar rat o Al/T1= 1.5) and 6.80 cc of a 2.23 molar solution of TiC1 5.40 cc of a for the 9 to h A1 ethyl Sesqwchlonde (having a 0.84 molar solution of AlEt Cl and 1 1.65 cc of a 1 4O molar rat) Al/Tl molar olution of poly N isopropylimino alane) Then We Stirred at a temperature of C for a The ratio b.w. of olefins/TiC1 was 90. The reduction of 5 hours- Of TiCl was 70% due to the l i in l n (h vi a After treating the product of the polymerization as in molar ratio Al/Ti 1.1) and due to the EtAl ses- P e e Obtained 50 g of dimer and 173 g of quichloride (having a Al/Ti ratio 1.0). Then we 400C+ oil. The conversion was of 86.1 b.w. and the stirred at the temperature of 25C for a time of 5 hours. yield f il WaS 66.8% b.w.

After treating the polymerization product as in the The characteristics of the obtained 400C+ oil are Example 1, we obtained 53 g of dimer and 169 g of reported in Table IV.

TABLE IV Characteristics Method 400C oil Specific gravity at 20C ASTM D 1481 1 0.8345 Refraction lndex. n ASTM D 1747 1.4680 Kinematic viscosity at 210F. cSt ASTM D 445 32.5 Kinematic viscosity at 100F, cSt ASTM D 445 209.4 Viscosity lndex ASTM D 2270 138/A 220/B Pour point, C ASTM D 97 400C oil. The conversion was 85.7% b.w. and the yield of oil of 65.2% b.w.

The 400C+ oil characteristics are reported in Table Said results show that by varying the molar ratio Al/Ti relative to the alane from 1.3 (of the Example 1) to 1.5

m we obtained oils with a higher viscosity.

TABLE III Characteristics Method 400C oil Specific gravity at 20C ASTM D 1481 0.8301

Refraction lndex, nfi" ASTM D 1747 1.4667

Kinematic viscosity at 210F, cSt ASTM D 445 10.81

Kinematic viscosity at F. cSt ASTM D 445 62.05

Viscosity lndex ASTM D 2270 l44/A 178/8 I Pour point. "C ASTM D 97 50 EXAMPLES 4 AND 5 They are similar to Example 1 varying only in the polymerization temperature.

In a 1 liter reactor, provided with a stirrer. dried, deaerated and flushed with dry nitrogen we introduced in the following order: 350 cc (259 g) of 97% l-decene, 6.80 cc of a 2.23 molar solution of TiCl 5.40 cc of a 0.84 molar solution AlEt Cl and 13,80 cc of 1.0 molar solution of poly-(N-isopropyliminoalane).

As in Example 1, the ratio by weight olefins/TiCl TABLE VI Characteristics Method 400C oil Specific gravity at C ASTM D 1481 0.8318 Refraction Index n ASTM D 1747 1.4674 Kinematic viscosity at 210F, cSt ASTM D 445 12.34 Kinematic viscosity at 100F, cSt ASTM D 445 71.40 Viscosity Index ASTM D 2270 l44/A-184/B Pour point. C ASTM D 97 50 was 90 and the reduction of TiCl was attributed for the 70% to the polyimino alane (having a molar ratio Al/Ti 1.3) and for the 30% to the Al ethyl sesquichloride (having a molar ratio 1.0).

The polymerization temperature was 50C in example 4 and 80C in the Example 5. The time was in both cases 5 hours.

The polymerization products were treated as in Example 1. In Example 4 we obtained a conversion of 58% and a yield of oil of In Example 5 the conversion was and the yield of oil 39%.

The characteristics of the two 400C+ oils were reported in the Table V.

' ,TABLE v Characteristics Method 400C oil example 4 Upon comparing these results with those of Example 1, we noticed that the addition of the solvent to the olefin of the feed reduces the oil viscosity, leaving the yield nearly unchanged.

EXAMPLE 7 In this example, as in the following ones, we employed as feed, a mixture of C C alpha-olefins from wax cracking.

To a 1 liter reactor provided with a stirrer, dried, deaerated and flushed with dry nitrogen, we introduced in the following order: 350 cc (260 g) of a mixture of commercial olefins C -C coming from wax crack- 400C oil example 5 ASTM D ASTM D ASTM D Specific gravity at 20C Refraction Index, n Kinematic viscosity at 210F, cSt

Kinematic viscosity at 100F, cSt Viscosity Index Pour Point. "C

ASTM D 516 ASTM D ASTM D The above results show that the increase of the temperature generates oils with minor yield and higher viscosity.

EXAMPLE 6 It is analogous to Example 1 with the only variation the presence of a solvent.

To a 1 liter reactor, provided with a stirrer, dried, deaerated and flushed with dry nitrogen we introduced in the following order, 350 cc (259 g) of 97% 1-decene and 350cc of benzene, 6.80 cc ofa 2.23 molar solution of TiCl 5.40 of a 0.84 molar solution of AlEt Cl and 13.80 cc of a 1.0 molar solution of poly-(N- isopropylimino alane).

As in Example 1, the ratio b.w. olefins/TiCl was 90 and the reduction of the TiCl was ascribed as to the polyiminoalane (having a molar ratio Al/Ti 1.3)

ing with a content of alpha-olefins of 87%, 6.80 cc of a 2.23 molar solution of TiC1 ,5.40 cc of 0.84 molar solution of AlEt Cl and 13.80 cc of a 1.0 molar solution of poly-(N-isopropylimino alane).

As in Example 1, the ratio by weight olefins/TiCL, was 90 and the reduction of TiCl was ascribed as 70% to the polyiminoalane (having a molar ratio Al/Ti 1,3) and 30% to Al Ethyl sesquichloride (having a molar ratio Al/Ti 1.0).

Then we stirred at a temperature of 25C for a time of 5 hours. 1

After treating the polymerization product as in example 1.27 g of dimer, and g of 400C+ oil were obtained. The conversion was 48.8% b.w. and the yield oil of 38.4% b.w.

The characteristics of the 400C+ oil so obtained were reported in Table VII.

TABLE VII Characteristics Specific gravity at 20C Refraction Index, n

ASTM D ASTM D TABLE VII Continued Characteristics Method 400C oil Kinematic viscosity at 210F, cSt ASTM D 445 25.31 Kinematic viscosity at 100F, cSt ASTM D 445 180.9 Viscosity Index ASTM D 2270 l36/A l83/B Pour point, C ASTM D 97 50 The above results show that even if we operated with It is to be noted that the monomer which does not the mixture of commercial C -C alpha-olefins from 10 take part in the reaction undergoes practically no hywax cracking, the obtained oils present good characdrogenation. teristics. The 400C+ oil was hydrogenated to saturate com- The yields are lower, as compared with those obpletely the olefinic double bonds. tained in Example 1 starting from l-decene, due to the The hydrogenation'was carried out in an autoclave presence of impurities in said mixture. by using a catalyst based on Pd on alumina in the following conditions: temperature 220C, pressure of hy- EXAMPLE 8 drogen 80 Kg/cm time 5 hours. The characteristics of It is analogous to example 7 with the only variation the hydrogenated oil are shown in Table IX.

TABLE IX Characteristics Method 400C hydrogenated oil Specific gravity at C ASTM D 1481 0.8404 Refraction Index, n ASTM D 1747 1.4690 Kinematic viscosity at 210F, cSt i 'ASTM D 445 24.42 Kinematic viscosity at 100F, cSt ASTM D 445 176.5 Viscosity Index I ASTM D 2270 l35/A-l79/B Pour point, C ASTM D 97 48 the decrease of the ratio by weight olefins/TiCl from The 400C+ hydrogenated oil which is shown in table 90 to 60. IX was subjected to a Shear Stability test with a Into a 1 litre reactor, provided with a stirrer dried, Raytheon sonic oscillator (ASTM D 2603-671) for a deaerated and flushed with dry nitrogen, we introtime of 15 minutes, calculating afterwards the variation duced, in the following order 350 cc (260 g) of a mixof the viscosity, measured at the temperature of 2 10F. ture of commercial C -C olefins coming from the The results appear in Table X. wax cracking, with a content of alpha-olefins of 87%, TABLE X 10.20 cc of a 2.23 molar solution of TiCl 8.10 cc of a 0.84 molar solution of AlEt Cl and 20.70 cc of a Kinematic viscosity, Kinematic viscosity 1 molar solution of poly-(N-isopropyliminoalane). cst at 0;.- Variation The ratio by weight olefins/TiCl, was 60. The reduc- I tion of the TiCl was ascribed as 70% to the 40 5mm"? test i Hydrogenated polyiminoalane (having a molar ratio Al/Ti 1.3) and Synthetic oil 2442 2168 014 30% to Al Ethyl sesquichloride (having a molar ratio Al/Ti 1.0). From the above data it is possible to deduce that the Then we stirred at the temperature of 25C for a time hydrogenatedsynthetic oil of Example 8 has good resisof 5 hours. tance to depolymerization.

After treating the polymerization product as in example 1.39 g of dimer and 135 g of 400c+ oil were ob- EXAMP 1 940 tained They were carried out as in Example 8, with a ratio The conversion was 67% by weight and the yield of y weight OlefinS/Ticl4 equal to but Varying from oil f the 52% 50 70/30 to /20 the ratio wherewith the two co-catalysts The characteristics of the obtained oil were reported reduce the k v i T bl VIII, Under these conditions we lowered from 1.3 to 1.2

TABLE VIII Characteristics Method 400C oil Specific gravity at 20C ASTM D 1481 0.8420 Refraction Index. n/F i ASTM D 1747 1.4704 Kinematic viscosity at 210F, cSt ASTM D 445 23.59 Kinematic viscosity at F, cSt ASTM D 445 169.0 Viscosity Index ASTM D 2270 i l36/A-l79/B Pour point, "C ASTM D 97 50 By comparing these results with those of Example 7 the ratio wherewith the complex PIA-TiCl is formed, we may deduce that, by operating with olefins C -C otherwise an oil with a high viscosity would be obfrom wax cracking, effect of the impurities on the 65 tained. yield may be limited by increasing the amount of the To the usual 1 liter reactor, dried, deaerated and catalyst. The characteristics of the oil remain satisfacflushed'with dry nitrogen we introduced in the followtory. mg order, 350 cc (260 g) ofthe mixture of C -C olefins coming from the wax cracking with a content of alpha-olefins of 87%; 10.2 cc ofa 2.3 molar solution of TiCl 5.4 cc of a 0.84 molar solution of AlEt Cl and 21.8 cc of 1.0 molar solution of poly-(N- isopropyliminoalane).

The ratio b.w. olefins/TiCL, was 60.

The reduction of the TiCl was ascribed as 80% due to the polyiminealane (having a molar ratio Al/Ti 1.2) and 20% to the Al Ethyl sesquichloride (having a molar ratio Al/Ti 1.0).

The polymerization temperature was 25C in Example 9 and 50C in Example 10. The time was in both cases 5 hours.

The polymerization products were treated as in Example l. 1n Example 9 we obtained a conversion of 83% with a yield of 400C+ oil of 63.5%.

In Example 10 the conversion was 79% and the yield of 400C+ oil 60%.

The characteristics of the two obtained 400C+ oils using the co-catalyst AlEt Cl in place of AlEt C1 Into a 1 liter reactor provided with a stirrer, dried, deaerated and flushed with dry nitrogen we introduced in the following order: 350 cc (260 g) of a mixture of commercial C -C olefins coming from the wax cracking with a content of alpha-olefins of 87%, 10.2 cc of a 2.23 molar solution of TiCl 4.25 cc of a 1.07 molar solution of AlEt Cl and 21.8 cc ofa 1.0 molar solution of poly-(N-isopropyliminoalane).

The ratio by weight olefins/TiCL, was 60.

The reduction of the TiCL, was ascribed as 80% due to the polyiminoalane (having a molar ratio Al/Ti 1.2) and to Al diethyl monochloride (having a molar ratio Al/Ti 1.0).

The polymerization temperature was C. The time was 5 hours. After treating the polymerization product as in Example 1, we obtained 47 g of dimer and 153 g of 400C-1- oil.

The conversion was of the 77% b.w. and the yield of The results of Example 9 show, in comparison with those of Example 8, that it is possible to increase fur- The characteristics of the produced oil are reported in the Table X11.

TABLE XII 400C Characteristics Method Oil Specific gravity at 20C ASTM D 1481 0.8410 Refraction Index, n ASTM D 1747 1.4698 Kinematic viscosity at 210F. cSt ASTM D 445 19.49 Kinematic viscosity at 100F. cSt ASTM D 445 135.1 Viscosity lndex ASTM D 2270 l36/A l75/B Pour point. "C ASTM D 97 50 EXAMPLE '1 1 It is similar to Example 9 with the difference that the polymerization of the C -C olefins was carried out by The results of the above example show that it is possible to substitute AlEt Cl with AlEt Cl.

We claim:

1. Process for the preparation of high quality lubricating oils through the polymerization of a member of the group consisting of pure normal alpha-olefins and of mixtures of commercial alpha-olefins having the general formula R CH CH in which R is an alkyl radical containing from 2 to 16 carbon atoms, wherein the catalytic system used for effecting the polymerization is a catalyst consisting of a compound of a transition metal selected from the group consisting of TiCl TiCl VCl and VOCl and two anionic coordinate v cocatalysts, consisting, respectively, of: (a) a linear polymer constituted by a polyiminic compound having the following general formula 3. Process according to claim 1, wherein the two cocatalysts which reduce the transition metal compound are in a ratio from /30 to /20.

4. Process according to claim 1 wherein the molar ratio between compound (a) and the compound of the transition metal is from 1.2 to 1.3, fixing at 1 the molar ratio between compound (b) and the transition metal compound.

5. Process according to claim 1, wherein the transition metal compound is TiCl 6. Process according to claim 1, wherein the ratio by weight of olefins/transition metal compound is between 10 and 500.

7. Process according to claim 1, wherein the reaction is carried out in the presence of a solvent selected from the group consisting of aromatic hydrocarbons, halogenated hydrocarbons and saturated hydrocarbons.

8. Process according to claim 1, wherein the polymerization temperature is from 0 to 200C.

UNITED STATES PATENT AND TRADEMARK OFFICE CERTIFICATE OF CORRECTION PATENT NO. 3,884,988 DATED May 20, 1975 INVENTOMS) I Pierleone Girotti, Renato Tesei and Telemaco Floris It is certified that error appears in the above-identified patent and that said Letters Patent are hereby corrected as shown below:

Column 3, line 10, after ."metal" insert a comma line 44, before "olefins" insert --feed-- Column 5, tableZ, line 10, "0.04" snould read "(0.04--

Column 6, line 37, "for the" should read --as-- line 39, delete "for the" Column 7, line 9, "l3,80" should read --13.80--

Column 8, line 1, delete "for" Column 13, line 13, before "an" (first occurrence) insert a comma Signed and Scaled this twenty-third D ay Of December I 9 75 [SEAL] A ttes t:

RUTH C. MASON Atlesting Officer 

1. PROCESS FOR THE PREPARATION OF HIGH QUALITY LUBRICATING OILS THROUGH TH POLYMERIZATION OF A MEMBER OF THE GROUP CONSISTING OF PURE NORMAL ALPHA-OLEFINS AND OF MIXTURES OF COMMERCIAL ALPHA-OLEFINS HAVING THE GENERAL FORMULA R - CH = CH2, IN WHICH R IS AN ALKYL RADICAL CONTAINING FROM 2 TO 16 CARBON ATOMS, WHEREIN THE CATALYTIC SYSTEM USED FOR EFFECTING THE POLYMERIZATION IS A CATALYST CONSISTING OF A COMPOUND OF A TRANSITION METAL SELECTED FROM THE GROUP CONSISTING OF TICL4, TICL3, VCL4 AND VOCL3 AND TWO ANIONIC COORDINATE COCATALYSTS, CONSISTING RESPECTIVELY, OF: (A) A LINEAR POLYMER CONSTITUTED BY A POLYIMINIC COMPOUND HAVING THE FOLLOWING GENERAL FORMULA
 2. Process according to claim 1 wherein the polymerization is carried out in a dry nitrogen atmosphere.
 3. Process according to claim 1, wherein the two cocatalysts which reduce the transition metal compound are in a ratio from 70/30 to 80/20.
 4. Process according to claim 1 wherein the molar ratio between compound (a) and the compound of the transition metal is from 1.2 to 1.3, fixing at 1 the molar ratio between compound (b) and the transition metal compound.
 5. Process according to claim 1, wherein the transition metal compound is TiCl4.
 6. Process according to claim 1, wherein the ratio by weight of olefins/transition metal compound is between 10 and
 500. 7. Process according to claim 1, wherein the reaction is carried out in the presence of a solvent selected from the group consisting of aromatic hydrocarbons, halogenated hydrocarbons and saturated hydrocarbons.
 8. Process according to claim 1, wherein the polymerization temperature is from 0* to 200*C. 